Hydrocracking Catalyst Containing Zeolite USY and Low Acidity and Large Domain Size Zeolite Beta

ABSTRACT

A hydrocracking catalyst comprising a zeolite beta having an average domain size from 800 to 1500 nm 2 ; a zeolite USY; a catalyst support; and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. The zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY, and, when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY, the zeolite beta has an OD acidity of 20 to 400 μmol/g, the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 with a corresponding zeolite USY content of from 0 to 5 wt. %. A process for hydrocracking a hydrocarbonaceous feedstock using the catalyst is also described as is a method for making the hydrocracking catalyst.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. Ser. No. 14/823,791, filed Aug. 11, 2015, entitled “MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING ZEOLITE BETA WITH LOW OD ACIDITY AND LARGE DOMAIN SIZE”, issued as U.S. Pat. No. 10,046,317, and a continuation of U.S. Ser. No. 14/823,807, filed Aug. 11, 2015, entitled “MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING ZEOLITE USY, AND ZEOLITE BETA WITH LOW ACIDITY AND LARGE DOMAIN SIZE”, issued as U.S. Pat. No. 10,040,058, herein incorporated by reference in their entireties.

This application is further related to U.S. Ser. No. 14/602,394, filed Jan. 22, 2015, entitled “IMPROVED NOBLE METAL ZEOLITE CATALYST FOR SECOND STAGE HYDROCRACKING”, herein incorporated by reference in its entirety.

TECHNICAL FIELD OF THE INVENTION

This application is directed to a hydrocracking catalyst, a composition thereof, a hydrocracking process using the hydrocracking catalyst, and a method of making the hydrocracking catalyst and composition thereof. The invention is useful in the hydrocracking of hydrocarbonaceous feedstocks to produce middle distillates.

BACKGROUND OF THE INVENTION

Improved hydrocracking catalysts, compositions thereof, and processes of making and using such catalysts are needed. Earlier hydrocracking catalysts have not provided the desired levels of activity and selectivity that are required to optimize the production of middle distillates.

SUMMARY OF THE INVENTION

The present invention is directed to a hydrocracking catalyst comprising a zeolite beta having an average domain size from 800 to 1500 nm², a zeolite USY, a catalyst support, and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. The OD acidity of the zeolite beta and the acid site distribution index (ASDI) of the zeolite USY have been determined to be important characteristics describing such catalysts. In general, the two zeolites in the hydrocracking catalyst are described according to the following conditions: the zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY, and, when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY, the zeolite beta has an OD acidity of 20 to 400 μmol/g, the zeolite beta content is from 0.5 to 10 wt. %, and the zeolite USY has an ASDI between 0.05 and 0.12 with a corresponding zeolite USY content of from 0 to 5 wt. %.

Also described is a process for hydrocracking a hydrocarbonaceous feedstock, comprising contacting the hydrocarbonaceous feedstock with the hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent that comprises middle distillates.

The invention is further directed to a method for making a hydrocracking catalyst, comprising mixing together a zeolite beta having an average domain size from 800 to 1500 nm²; a zeolite USY; a catalyst support; and enough liquid to form an extrudable paste, wherein the zeolite beta, the catalyst support, and the zeolite USY satisfy the conditions noted herein; extruding the extrudable paste to form an extrudate base; impregnating the extrudate base with a metal impregnation solution containing at least one metal selected from the group consisting of elements from Group 6 and Group 8 through 10 of the Periodic Table to make a metal-loaded extrudate; and post-treating the metal-loaded extrudate by subjecting the metal-loaded extrudate to drying and calcination. In accordance with this method, the hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.).

The present invention may suitably comprise, consist of, or consist essentially of, the elements in the claims, as described herein.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a transmission electron microscopy (TEM) image showing the agglomerate crystals of the H-BEA-150 zeolite beta used in the preparation of the hydrocracking catalysts in the examples.

FIG. 2 is a chart of the domain measurements made on two samples of zeolite beta.

FIG. 3 is a chart of the average domain sizes of two samples of zeolite beta.

GLOSSARY

“Hydrocracking” refers to a process in which hydrogenation and dehydrogenation accompanies the cracking/fragmentation of hydrocarbons, e.g., converting heavier hydrocarbons into lighter hydrocarbons, or converting aromatics and/or cycloparaffins(naphthenes) into non-cyclic branched paraffins.

“Cut point” refers to the temperature on a True Boiling Point (“TBP) curve at which a predetermined degree of separation is reached.

“TBP” refers to the true boiling point of a hydrocarbonaceous feed or product, as determined by ASTM D2887-13.

“Hydrocarbonaceous” means a compound or substance that contains hydrogen and carbon atoms, and which can include heteroatoms such as oxygen, sulfur, or nitrogen.

“Distillates” include the following products:

Typical Cut Points, ° F. (° C.), Products North American Market Light Naphtha C₅-180 (C₅-82) Heavy Naphtha 180-300 (82-149) Jet 300-380 (149-193) Kerosene 380-530 (193-277) Diesel 530-700 (277-371)

“Middle distillates” include jet kerosene and diesel products, as defined by their typical cut points, above.

“Heavy middle distillates” refers to products having a TBP of 380-700° F. (193-371° C.).

“Finished catalyst” refers to the hydrocracking catalyst composition comprising all of its components and after all of the processing and any post-processing steps used to manufacture it.

“LHSV” means liquid hourly space velocity.

“SCF/B” refers to a unit of standard cubic foot of gas (e.g., nitrogen, hydrogen, air, etc) per barrel of hydrocarbonaceous feed.

“Zeolite beta” refers to zeolites having a 3-dimensional crystal structure with straight 12-membered ring channels with crossed 12-membered ring channels, and having a framework density of about 15.3 T/1000 Å³. Zeolite beta has a BEA framework as described in Ch. Baerlocher and L. B. McCusker, Database of Zeolite Structures: http://www.iza-structure.org/databases/

“SiO₂/Al₂O₃ ratio (SAR) is determined by inductively coupled plasma (ICP) elemental analysis. A SAR of infinity means there is no aluminum in the zeolite, i.e., the mole ratio of silica to alumina is infinity. In that case, the zeolite is comprised of essentially all silica.

“Zeolite USY” refers to ultra-stabilized Y zeolite. Y zeolites are synthetic faujasite (FAU) zeolites having a SAR of 3 or higher. Y zeolite can be ultra-stabilized by one or more of hydrothermal stabilization, dealumination, and isomorphous substitution. Zeolite USY can be any FAU-type zeolite with a higher framework silicon content than a starting (as-synthesized) Na—Y zeolite precursor.

“Catalyst support” refers to a material, usually a solid with a high surface area, to which a catalyst is affixed.

“Periodic Table” refers to the version of the IUPAC Periodic Table of the Elements dated Jun. 22, 2007, and the numbering scheme for the Periodic Table Groups is as described in Chemical and Engineering News, 63(5), 27 (1985).

“OD acidity” refers to the amount of bridged hydroxyl groups exchanged with deuterated benzene at 80° C. by Fourier transform infrared spectroscopy (FTIR). OD acidity is a measure of the Brönsted acid sites density in a catalyst. The extinction coefficient of OD signals was determined by analysis on a standard zeolite beta sample calibrated with ¹H magic-angle spinning nuclear magnetic resonance (MAS NMR) spectroscopy. A correlation between the OD and OH extinction coefficients was obtained using the relationship: ε_((−OD))=0.62*ε_((−OH)).

“Domain Size” is the calculated area, in nm², of the structural units observed and measured in zeolite beta catalysts. Domains are described by Paul A. Wright et. al., “Direct Observation of Growth Defects in Zeolite Beta”, JACS Communications, published on web Dec. 22, 2004. The method used to measure the domain sizes of zeolite beta is further described herein.

“Acid site distribution index (ASDI)” is an indicator of the hyperactive site concentration of a zeolite. In some embodiments, the lower the ASDI the more likely the zeolite will have a greater selectivity towards the production of heavier middle distillate products.

“Amorphous silica aluminate (ASA)” refers to a synthetic material having some of the alumina present in tetrahedral coordination as shown by nuclear magnetic resonance imaging. ASA can be used as a catalyst or catalyst support. Amorphous silica alumina contains sites which are termed Brönsted acid (or protic) sites, with an ionizable hydrogen atom, and Lewis acid (aprotic), electron accepting sites and these different types of acidic site can be distinguished by the ways in which, say, pyridine attaches.

“Pseudo-boehmite alumina refers to an aluminum compound with the chemical composition AIO(OH). Pseudo-boehmite alumina consists of finely crystalline boehmite with a higher water content than boehmite.

“Polycyclic index” (PCI) refers to a calculated value that relates to the amount of polycyclic aromatics that are in a hydrocarbon feed. The test method to determine PCI is ASTM D6379-11. PCI is useful in evaluating feedstocks for hydroprocessing. PCI is measured using UV-spectroscopy and is calculated as follows:

PCI={[Absorbance @385 nm−(0.378×Absorbance@435 nm)]/115×c}×1000

where c is the original concentration of the sample in solvent in g/cm³.

“API gravity” refers to the gravity of a petroleum feedstock or product relative to water, as determined by ASTM D4052-11.

DETAILED DESCRIPTION

This invention concerns the discovery that the unique combination of zeolite beta having a defined OD acidity and a defined average domain size with a zeolite USY in a specified proportion provides a hydrocracking catalyst having improved hydrocracking performance. The combination of these two zeolites in a hydrocracking catalyst gives improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.). The hydrocracking catalyst can also provide improved activity, such as from 1 to 20° F. at 60% conversion compared to other hydrocracking catalysts that do not have the unique combination of zeolites disclosed herein.

Hydrocracking Catalyst Composition—Zeolite Beta:

The zeolite beta has an average domain size from 800 to 1500 nm². In one embodiment, the OD acidity of the zeolite beta is from 20 to 50, more particularly from 30 to 40 μmol/g, when the wt. % content of the zeolite beta in the hydrocracking catalyst is less than the zeolite USY wt. % content. In another embodiment, the OD acidity of the zeolite beta is from 20 to 400, more particularly from 30 to 100 μmol/g, when the wt. % content of the zeolite beta in the hydrocracking catalyst is greater than the zeolite USY wt. % content.

In addition, when the wt. % content of the zeolite beta in the hydrocracking catalyst is greater than the zeolite USY wt. % content, the zeolite beta content is from 0.5 to 10 wt. % of the catalyst and the zeolite USY content is from 0 to 5 wt. % of the catalyst. More particularly, the zeolite beta content is from 1 to 5 wt. % higher than the wt. % content of the zeolite USY.

In one embodiment the zeolite beta is synthetically manufactured using organic templates. Examples of three different zeolite betas are described in Table 1.

TABLE 1 Zeolite SiO₂/Al₂O₃ Molar OD Acidity Betas Ratio (SAR) μmol/g H-BEA-35 35 304 H-BEA-150 (ZE0090) 150  36 CP811C-300 (ZE0106) 300 Not measured

The total OD acidity was determined by H/D exchange of acidic hydroxyl groups by FTIR spectroscopy. The method to determine the total OD acidity was adapted from the method described in the publication by Emiel J. M. Hensen et. al., J. Phys. Chem., C2010, 114, 8363-8374. Prior to FTIR measurement, the sample was heated for one hour at 400-450° C. under vacuum <1×10⁻⁵ Torr. Then the sample was dosed with C₆D₆ to equilibrium at 80° C. Before and after C₆D₆ dosing, spectra were collected for OH and OD stretching regions.

The average domain size was determined by a combination of transmission electron microscopy (TEM) and digital image analysis, as follows:

I. Zeolite Beta Sample Preparation:

The zeolite beta sample was prepared by embedding a small amount of the zeolite beta in an epoxy and microtoming. The description of suitable procedures can be found in many standard microscopy text books.

Step 1. A small representative portion of the zeolite beta powder was embedded in epoxy. The epoxy was allowed to cure.

Step 2. The epoxy containing a representative portion of the zeolite beta powder was microtomed to 80-90 nm thick. The microtome sections were collected on a 400 mesh 3 mm copper grid, available from microscopy supply vendors.

Step 3. A sufficient layer of electrically-conducting carbon was vacuum evaporated onto the microtomed sections to prevent the zeolite beta sample from charging under the electron beam in the TEM.

II. TEM Imaging:

Step 1. The prepared zeolite beta sample, described above, was surveyed at low magnifications, e.g., 250,000-1,000,000× to select a crystal in which the zeolite beta channels can be viewed.

Step 2. The selected zeolite beta crystals were tilted onto their zone axis, focused to near Scherzer defocus, and an image was recorded 2,000,000×.

III. Image Analysis to Obtain Average Domain Size (nm²):

Step 1. The recorded TEM digital images described previously were analyzed using commercially available image analysis software packages.

Step 2. The individual domains were isolated and the domain sizes were measured in nm². The domains where the projection was not clearly down the channel view were not included in the measurements.

Step 3. A statistically relevant number of domains were measured. The raw data was stored in a computer spreadsheet program.

Step 4. Descriptive statistics, and frequencies were determined—The arithmetic mean (d_(a)y), or average domain size, and the standard deviation (s) were calculated using the following equations:

The average domain size, d _(av)=(ån _(i) d _(i))/(ån _(i))

The standard deviation, s=(å(d _(i)−_(av))⁰/(ån _(i)))^(1/2)

In one embodiment the average domain size is from 900 to 1250 nm², such as from 1000 to 1150 nm².

Hydrocracking Catalyst Composition—Zeolite USY:

The hydrocracking catalyst may generally comprise a zeolite USY in an amount that that is greater or less than the amount of the zeolite beta in accordance with the conditions noted herein for each zeolite.

In one embodiment according to these conditions, the zeolite USY content is not generally limited to a specified range when the wt. % content of the zeolite beta in the hydrocracking catalyst is less than the zeolite USY wt. % content. In another embodiment according to these conditions, the zeolite USY content is from 0 to 5 wt. % when the wt. % content of the zeolite beta in the hydrocracking catalyst is greater than the zeolite USY wt. % content, while the wt. % content of the zeolite beta is from 0.5 to 10 wt. % of the catalyst.

In one embodiment, the zeolite USY has an acid site distribution index (ASDI) that favors the production of heavy middle distillates. For example, the zeolite USY can have an ASDI from 0.05 to 0.12. ASDI is determined by H/D exchange of acidic hydroxyl groups by FTIR spectroscopy, as described previously. Brönsted acid sites density was determined by using the integrated area of peak 2676 cm⁻¹ as the first high frequency OD (HF), 2653 cm⁻¹ as the 2^(nd) high frequency OD (HF′), 2632 cm⁻¹ and 2620 cm⁻¹ as the first low frequency OD (LF) and 2600 cm⁻¹ as the 2^(nd) low frequency OD (LF′). The acid site distribution index factor was determined by the following equation: ASDI=(HF′+LF′)/(HF+LF); which reflects the hyperactive acid sites content in the zeolite sample. In one embodiment the zeolite USY has a total Brönsted acid sites determined by FTIR after H/D exchange of 0.080 to 0.200 mmol/g.

In one embodiment, when the zeolite beta content is less than the zeolite USY, the hydrocracking catalyst has a weight ratio of the zeolite beta to the zeolite USY is from 0.10 to 0.95.

In one embodiment, when the wt. % of the zeolite beta is greater than the wt. % of the zeolite USY in the hydrocracking catalyst, the wt. % of the zeolite beta can be from 0.45 to 9.95 wt. % greater than the wt. % of the zeolite USY. More particularly, according to this embodiment, the wt. % of the zeolite beta may be from 1 to 5 wt. % higher than the wt. % of the zeolite USY. The hydrocracking catalyst may have a weight ratio of the zeolite USY to the zeolite beta that is less than 0.90, such as from 0.01 to 0.80, or from 0.02 to 0.48.

Hydrocracking Catalyst Composition—Catalyst Support:

The hydrocracking catalyst comprises a catalyst support. The catalyst support can be inert or can participate in the catalytic reactions performed by the hydrocracking catalyst. Typical catalyst supports include various kinds of carbon, alumina, and silica. In one embodiment, the catalyst support comprises an amorphous silica aluminate. In one embodiment, the catalyst support comprises an amorphous silica aluminate and a second support material, particularly when the content of the zeolite beta in the hydrocracking catalyst is less than the zeolite USY wt. % content.

In one embodiment, the amorphous silica aluminate (ASA) has greater thermal stability than high purity aluminas. Examples of suitable amorphous silica aluminates are SIRAL® ASAs, described below:

TABLE 2 SIRAL SIRAL SIRAL SIRAL SIRAL Typical Properties SIRAL 1 5 10 20 30 40 Al₂O₃ + SiO₂ % 75 75 75 75 75 75 Loss on Ignition (LOI) % 25 25 25 25 25 25 Al₂O₃:SiO₂ % 99:1 95:5 90:10 80:20 70:30 60:40 C % 0.2 0.2 0.2 0.2 0.2 0.2 Fe₂O₃ % 0.02 0.02 0.02 0.02 0.02 0.02 Na₂O % 0.005 0.005 0.005 0.005 0.005 0.005 Loose bulk density [g/l] 600-800 450-650 400-600 300-500 250-450 250-450 Particle size (d₅₀) [μm] 50 50 50 50 50 50 Surface area (BET)* [m²/g] 280 370 400 420 470 500 Pore volume* [ml/g] 0.50 0.70 0.75 0.75 0.80 0.90 *Brunauer, Emmett and Teller (BET) theory and specific surface area determination, after activation at 550° C. for 3 hours. SIRAL ® is a registered trademark of SASOL.

Examples of the second support material can include kieselguhr, alumina, silica, and silica-alumina. Other examples of the second support material include alumina-boria, silica-alumina-magnesia, silica-alumina-titania and materials obtained by adding zeolites and other complex oxides thereto. In one embodiment, the second support material is porous, and comprises a natural clay or a synthetic oxide. The second support material can be selected to provide adequate mechanical strength and chemical stability at the reaction conditions under which the hydrocracking catalyst is employed.

In one embodiment, the second support material comprises a pseudo-boehmite alumina. Examples of pseudo-boehmite alumina are CATAPAL® high purity aluminas. CATAPAL® is a registered trademark of SASOL. Typical properties of the CATAPAL high purity aluminas are summarized below:

TABLE 3 Typical CATAPAL CATAPAL CATAPAL CATAPAL Properties B C1 D 200 Al₂O₃, wt % 72 72 76 80 Na₂O, wt % 0.002 0.002 0.002 0.002 Loose Bulk 670-750 670-750 700-800 500-700 Density, g/l Packed Bulk  800-1100  800-1100  800-1100 700-800 Density, g/l Average 60 60 40 40 Particle size (d₅₀), μm Surface Area* 250 230 220 100 (BET), m²/g Pore Volume*, 0.50 0.50 0.55 0.70 ml/g Crystal size, 4.5 5.5 7.0 40 nm *Surface area and pore volume were determined after activation at 550° C. for 3 hours.

The metal used in the hydrocracking catalyst is selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table, and mixtures thereof. In one embodiment, each metal is selected from the group consisting of nickel (Ni), palladium (Pd), platinum (Pt), cobalt (Co), iron (Fe), chromium (Cr), molybdenum (Mo), tungsten (W), and mixtures thereof. Examples of mixtures of metals that can be used include Ni/Mo/W, Ni/Mo, Ni/W, Co/Mo, Co/W, Co/W/Mo, Ni/Co/W/Mo, and Pt/Pd. In another embodiment, the hydrocracking catalyst contains at least one Group 6 metal and at least one metal selected from Groups 8 through 10 of the periodic table. Exemplary metal combinations include Ni/Mo/W, Ni/Mo, Ni/W, Co/Mo, Co/W, Co/W/Mo and Ni/Co/W/Mo.

In one embodiment, the total amount of a metal oxide in the hydrocracking catalyst is from 0.1 wt. % to 90 wt. % based on the bulk dry weight of the finished hydrocracking catalyst. In one embodiment, the hydrocracking catalyst contains from 2 wt. % to 10 wt. % of nickel oxide and from 8 wt. % to 40 wt. % of tungsten oxide based on the bulk dry weight of the finished hydrocracking catalyst.

In one embodiment, the finished hydrocracking catalyst will have the following composition:

0.5 to 10 wt % zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm2, 0 to 5 wt % zeolite USY having an ASDI between 0.05 and 0.12, with the wt % zeolite beta being greater than the wt % zeolite USY, 3 to 6 wt % nickel oxide, and from 15 to 35 wt % of tungsten oxide. Additionally, in one embodiment, the finished hydrocracking catalyst can contain an organic acid in an amount wherein the organic acid/Ni molar ratio is from 0 to 2.

The hydrocracking catalyst may additionally contain one or more promoters selected from the group consisting of phosphorous (P), boron (B), fluorine (F), silicon (Si), aluminum (Al), zinc (Zn), manganese (Mn), and mixtures thereof. The amount of promoter in the hydrocracking catalyst can be from 0 wt. % to 10 wt. % based on the bulk dry weight of the finished hydrocracking catalyst. In one embodiment, the amount of promoter in the hydrocracking catalyst is from 0.1 wt. % to 5 wt. % based on the bulk dry weight of the finished hydrocracking catalyst.

In one embodiment, the hydrocracking catalyst is in the form of extruded pellets (extrudates) that have an extruded pellet diameter of 10 mm or less, such as from 1.0 to 5.0 mm. In one embodiment, the extruded pellet has a length-to-diameter ratio of 10 to 1. Examples of other types and sizes of pellets used for the hydrocracking catalysts are 1 to 10 mm diameter spheres; 1 to 10 mm diameter cylinders with a length-to-diameter ratio of 4 to 1; 1 to 10 mm asymmetric shapes (including quadrolobes), and up to 10 mm diameter hollow cylinders or rings.

Hydrocracking Catalyst Preparation

The hydrocracking catalyst can be prepared by: a) mixing the zeolite beta, the zeolite USY (when used), the catalyst support (e.g., an amorphous silica aluminate and the second support material according to one embodiment), and enough liquid to form an extrudable paste that forms an extrudate base; b) impregnating the extrudate base with a metal impregnation solution containing at least one metal to make a metal-loaded extrudate; and c) post-treating the metal-loaded extrudate by subjecting the metal-loaded extrudate to drying and calcination.

In one embodiment, the method for making a hydrocracking catalyst, comprises:

mixing together a zeolite beta having an OD acidity of 20 to 50 μmol/g; optionally, a zeolite USY; an amorphous silica aluminate; a second support material; and enough liquid to form an extrudable paste;

extruding the extrudable paste to form an extrudate base;

impregnating the extrudate base with a metal impregnation solution containing at least one metal selected from the group consisting of elements from Group 6 and Group 8 through 10 of the Periodic Table to make a metal-loaded extrudate; and

post-treating the metal-loaded extrudate by subjecting the metal-loaded extrudate to drying and calcination; wherein the hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.).

In one embodiment, the method for making a hydrocracking catalyst comprises:

mixing together a zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm²; a zeolite USY having an ASDI between 0.05 and 0.12; a catalyst support; and enough liquid to form an extrudable paste; wherein a wt % of the zeolite beta is greater than a second wt % of the zeolite Y;

extruding the extrudable paste to form an extrudate base;

impregnating the extrudate base with a metal impregnation solution containing at least one metal selected from the group consisting of elements from Group 6 and Group 8 through 10 of the Periodic Table to make a metal-loaded extrudate; and

post-treating the metal-loaded extrudate by subjecting the metal-loaded extrudate to drying and calcination; wherein the hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.).

In one embodiment the liquid used to form the paste is a diluted HNO₃ acid aqueous solution with from 0.5 to 5 wt % HNO₃. Water or a mild acid may also be used in certain embodiments.

Prior to impregnation, the extrudate base can be dried at a temperature between 90° C. (194° F.) and 150° C. (302° F.) for 30 minutes to 3 hours. The dried extrudate base can then be calcined at one or more temperatures between 350° C. (662° F.) and 700° C. (1292° F.).

In one embodiment, the metal impregnation solution is made by dissolving metal precursors in a solvent. Suitable solvents include water, C₁-C₃ alcohols, ethers, and amines. In one embodiment, the solvent is deionized water. The concentration of the impregnation solution can be determined by the pore volume of the catalyst support and by the selected metal loading. In one embodiment, the extrudate base is exposed to the impregnation solution for 0.1 to 10 hours.

In one embodiment, impregnation of at least one of the metals is achieved in the presence of a modifying agent that can be selected from the group consisting of compounds represented by structures (1) through (4), including condensated forms thereof:

wherein:

(1) R1, R2 and R3 are independently selected from the group consisting of hydrogen; hydroxyl; methyl; amine; and linear or branched, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 alkenyl groups, C1-C3 hydroxyalkyl groups, C1-C3 alkoxyalkyl groups, C1-C3 aminoalkyl groups, C1-C3 oxoalkyl groups, C1-C3 carboxyalkyl groups, C1-C3 aminocarboxyalkyl groups and C1-C3 hydroxycarboxyalkyl groups;

(2) R4 through R10 are independently selected from the group consisting of hydrogen; hydroxyl; and linear or branched, substituted or unsubstituted C2-C3 carboxyalkyl groups; and

(3) R11 is selected from the group consisting of linear or branched, saturated and unsaturated, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 hydroxyalkyl groups, and C1-C3 oxoalkyl groups.

Representative examples of modifying agents useful in this embodiment include 2,3-dihydroxy-succinic acid, ethanedioic acid, 2-hydroxyacetic acid, 2-hydroxy-propanoic acid, 2-hydroxy-1,2,3-propanetricarboxylic acid, methoxyacetic acid, cis-1,2-ethylene dicarboxylic acid, hydroethane-1,2-dicarboxyic acid, ethane-1,2-diol, propane-1,2,3-triol, propanedioic acid, and α-hydro-w-hydroxypoly(oxyethylene).

In an alternate embodiment, deposition of at least one of the metals is achieved in the presence of a modifying agent selected from the group consisting of N,N′-bis(2-aminoethyl)-1,2-ethane-diamine, 2-amino-3-(1H-indol-3-yl)-propanoic acid, benzaldehyde, [[(carboxymethyl)imino]bis(ethylenenitrilo)]-tetra-acetic acid, 1,2-cyclohexanediamine, 2-hydroxybenzoic acid, thiocyanate, thiosulfate, thiourea, pyridine, and quinoline.

When used, the modifying agent can impede metal aggregation, thereby enhancing the activity and selectivity of the catalyst.

For each embodiment described herein, the amount of modifying agent in the pre-calcined hydrocracking catalyst can be from 0 wt % to 18 wt % based on the bulk dry weight of the hydrocracking catalyst.

In one embodiment, the metal impregnation solution can additionally comprise a peptizing agent. Examples of peptizing agents are organic acids such as pyruvic acid, levulinic acid, acetic acid, 2-ketogulonic acid, keto-gluconic acid, thioglycolic acid, 4-acetylbutyric acid, 1,3-acetonedicarboxylic acid, 3-oxo propanoic acid, 4-oxo butanoic acid, 2,3-diformyl succinic acid, citric acid, 5-oxo pentanoic acid, 4-oxo pentanoic acid, formic acid, propionic acid, butyric acid, valeric acid, caproic acid, enantic acid, caprylic acid, pelargonic acid, capric acid, undecylic acid, lauric acid, tridecylic acid, benzoic acid, salicylic acid, glutaric acid, adipic acid, pimelic acid, azelaic acid, phtalic acid, isophtalic acid, lactic acid, ethyl glyoxylate, glycolic acid, glucose, glycine, oxamic acid, glyoxylic acid, ethylenediaminetetraacetic acid (EDTA), nitrilotriacetic acid, N-methylaminodiacetic acid, iminodiacetic acid, diglycolic acid, malic acid, gluconic acid, acetylacetone, tartaric acid, aconitic acid, suberic acid, tricarballylic acid, malonic acid, succinic acid, and glycolic acid.

In one embodiment the metal-loaded extrudate is dried at one or more temperatures in the range of 38° C. (100° F.) to 149° C. (300° F.) for 0.1 to 10 hours. The dried metal-loaded extrudate can be further calcined at one or more temperatures from 316° C. (600° F.) to 649° C. (1200° F.), with purging excess dry air, for 0.1 to 10 hours.

Hydrocracking Overview

The hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.) from a wide variety of hydrocarbonaceous feedstocks. Examples of hydrocarbonaceous feedstocks include those that could be considered disadvantaged feedstocks that would not normally be conducive for making a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.) using a conventional one- or two-stage hydrocracking process. Suitable hydrocarbonaceous feed stocks that can be used can include visbroken gas oils, heavy coker gas oils, gas oils derived from residue hydrocracking or residue desulfurization, other thermally cracked oils, de-asphalted oils, Fischer-Tropsch derived feedstocks, cycle oils from a fluid catalytic cracking (FCC) unit, heavy coal-derived distillates, coal gasification byproduct tars, heavy shale-derived oils, organic waste oils such as those from pulp or paper mills or from waste biomass pyrolysis units.

Table 4 lists some typical physical properties for a hydrocarbonaceous feedstock that can be used.

TABLE 4 Property Range API Gravity 13.5-30.0 N, ppm  0.5-2,000 S, wt % 0-5 Polycyclic Index (PCI) 1500-8000 TBP Range, ° F. (° C.)   700-1200° F.    (371-649° C.)

Table 5 lists some typical hydrocracking process conditions that can be used.

TABLE 5 Property Range Liquid Hourly Space Velocity (LHSV), hr⁻¹ 0.1-5    H₂ partial pressure, psig (kPa) 800-3,500 (5516-24,132) H₂ Consumption Rate, SCF/B  200-20,000 H₂ Recirculation Rate, SCF/B  50-5,000 Operating Temperature   200-450° C.  (392-842° F.) Conversion (wt %) 30-90 

Depending on the feedstock, target product slate and amount of available hydrogen, the catalyst described herein can be used alone or in combination with other conventional hydrocracking catalysts.

In one embodiment, the catalyst is deployed in one or more fixed beds in a single stage hydrocracking unit, with or without recycle (once-through). Optionally, the single-stage hydrocracking unit may employ multiple single-stage units operated in parallel.

In one embodiment, the catalyst is deployed in one or more beds or units in a two-stage hydrocracking unit, with and without intermediate stage separation, and with or without recycle. Two-stage hydrocracking units can be operated using a full conversion configuration (meaning all of the hydrotreating and hydrocracking is accomplished within the hydrocracking loop via recycle). This embodiment may employ one or more distillation units within the hydrocracking loop for the purpose of stripping off product prior to the second stage hydrocracking step or prior to recycle of the distillation bottoms back to the first and/or second stage.

Two stage hydrocracking units can also be operated in a partial conversion configuration (meaning one or more distillation units are positioned within hydrocracking loop for the purpose of stripping of one or more streams that are passed on for further hydroprocessing). Operation of the hydrocracking unit in this manner allows a refinery to hydroprocess highly disadvantaged feedstocks by allowing undesirable feed components such as the polynuclear aromatics, nitrogen and sulfur species (which can deactivate hydrocracking catalysts) to pass out of the hydrocracking loop for processing by equipment better suited for processing these components, e.g., an FCC unit.

In one embodiment, the catalyst is used in the first stage and optionally the second stage of a partial conversion, two-stage hydrocracking configuration which is well suited for making at least one middle distillate and a heavy vacuum gas fluidized catalytic cracking feedstock (HVGO FCC), by:

(a) hydrocracking a hydrocarbonaceous feedstock to produce a first stage hydrocracked effluent;

(b) distilling the hydrocracked feedstock by atmospheric distillation to form at least one middle distillate fraction and an atmospheric bottoms fraction;

(c) further distilling the atmospheric bottoms fraction by vacuum distillation to form a side-cut vacuum gas oil fraction and a heavy vacuum gas oil FCC feedstock;

(d) hydrocracking the side-cut vacuum gas oil fraction to form a second stage hydrocracked effluent; and

(e) combining the second stage hydrocracked effluent with the first stage hydrocracked effluent.

The refinery configuration illustrated above has several advantages over conventional two-stage hydrocracking schemes. First, in this configuration, the catalyst and operating conditions of the first stage are selected to yield a HVGO FCC stream having only the minimum feed qualities necessary to produce FCC products which meet the established commercial specifications. This is in contrast to a conventional two-stage hydrocracking scheme where the first stage hydrocracking unit is operated at a severity necessary to maximize distillate yield which, in turn, requires the unit to be operated at more severe conditions (which requires more hydrogen and reduces the life of the catalyst).

Second, in this optional configuration, the side-cut vacuum gas oil (VGO) sent to the second stage hydrocracker unit is cleaner and easier to hydrocrack than a conventional second stage hydrocracker feed. Therefore, higher quality middle distillate products can be achieved using a smaller volume of second stage hydrocracking catalyst which, in turn, allows for the construction of a smaller hydrocracker reactor and consumption of less hydrogen. The second stage hydrocracking unit configuration reduces construction cost, lowers catalyst fill cost and operating cost.

Products Made by Hydrocracking

The hydrocracking catalyst can produce significantly increased yields of middle distillates. In another embodiment, the hydrocracking catalyst can also provide reduced yields of products having a cut point below 380° F. In one embodiment, the hydrocracked effluent comprises at greater than 50 vol % to 95 vol % of a heavy middle distillate having a TBP of 380-700° F. (193-371° C.). In one embodiment, the hydrocracked effluent comprises at least 75 vol % to 99 vol % hydrocarbons having a TBP less than 700° F. (371° C.).

In one embodiment, the hydrocracking catalyst produces light naphtha and heavy naphtha, but the yields can be reduced compared to earlier hydrocracking catalysts not comprising the zeolite beta having an OD acidity of 20 to 50 μmol/g and an average domain size from 800 to 1500 nm².

In one embodiment, the hydrocracking catalyst produces light naphtha and heavy naphtha, but the yields of light naphtha and heavy naphtha can be reduced compared to earlier hydrocracking catalysts not comprising the zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm².

EXAMPLES

The following examples illustrate results obtained in accordance with the invention. Examples 1 to 7 concern catalysts according to the invention wherein the zeolite beta content in the catalyst is less than the zeolite USY content, whereas Examples 1a to 7a concern catalysts according to the invention wherein the zeolite beta content in the catalyst is greater than the zeolite USY content.

Example 1: Comparative Catalysts

Three commercial catalyst samples were obtained. They were identified as A, B, and C. The composition of these comparative catalysts are summarized in Table 7.

Example 2: Preparation of Catalyst Sample D

Catalyst sample D was prepared by combining 2.3 wt % H-BEA-150 zeolite, 9.0 wt % USY zeolite, 72.6 wt % amorphous silica alumina (ASA) powder, and 16.2 wt % pseudo-boehmite alumina; and mixing them well. The H-BEA-150 zeolite was a zeolite beta that was obtained from SUD CHEMIE. The USY zeolite was obtained from Zeolyst. The USY zeolite had an acid site distribution index (ASDI) of 0.086. Additional properties of the USY zeolite are summarized in Table 6.

TABLE 6 Brönsted acid sites determined by FTIR after H/D exchange (mmol/g) HF(OD) 0.076 HF′(OD) 0.005 LF(OD) 0.034 LF′(OD) 0.003 Total 0.118 ASDI 0.086

The ASA powder was Siral-30 obtained from Sasol. The pseudo-boehmite alumina was CATAPAL C1 from Sasol.

To this mixture described above, a diluted HNO₃ acid aqueous solution (3 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ (1.59 mm) asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 3.8 wt % NiO and 25.3 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for 1 hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished catalyst sample D is shown in Table 7.

Example 3: Preparation of Catalyst Sample E

Catalyst sample E was prepared similar to the process described in Example 2. 5.6 wt % H-BEA-150 zeolite, 16.2 wt % USY zeolite, 55.6 wt % ASA powder, and 22.6 wt % pseudo-boehmite alumina powder were combined and mixed well. To this mixture, a diluted HNO₃ acid aqueous solution (3 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 3.8 wt % NiO and 25.3 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for 1 hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished catalyst sample E is shown in Table 7.

Example 4: Preparation of Catalyst Sample F

Catalyst sample F was prepared by the same procedure as used to make catalyst sample E, except H-BEA-35 (SUD CHEMIE) was used instead of H-BEA-150. The composition of this finished catalyst sample F is shown in Table 7.

Example 5: Preparation of Catalyst Sample G

Catalyst sample G was prepared similar to the process described in Example 2. 11.3 wt % H-BEA-150 zeolite, 45.1 wt % USY zeolite, 27.6 wt % ASA powder, and 16.0 wt % pseudo-boehmite alumina powder were combined and mixed well. The pseudo-boehmite alumina was CATAPAL B from Sasol. To this mixture, a diluted HNO₃ acid aqueous solution (3 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using an impregnation solution containing ammonium metatungstate and nickel carbonate at concentrations to achieve the target metal loadings of 5.0 wt % NiO and 29.0 wt % WO₃, based on the bulk dry weight of the finished catalyst. The impregnation solution also contained 10.3 grams of citric acid. The metal impregnated extruded catalyst was dried at 212° F. (100° C.) for two hours. The composition of this finished catalyst sample G is shown in Table 7.

TABLE 7 Catalyst Compositions Base Base Catalyst Component Case A D Case B E F Base Case C G Zeolite beta H-BEA-150, wt % 0 1.6 0 4 0 0 8 Zeolite beta H-BEA-35, wt % 0 0 0 0 4 0 0 USY Zeolite, wt % 6 6.4 20 16 16 40 32 Weight Ratio beta/USY 0 0.25 0 0.25 0.25 0 0.25 NiO, wt % 3.8 3.8 3.8 3.8 3.8 3.8 5 WO₃, wt % 25.3 25.3 25.3 25.3 25.3 25.3 29

Example 6: Comparison of Catalyst Performance

The example catalysts described above were used to process a typical Middle Eastern VGO feedstock. The properties of this feedstock are described in Table 8.

TABLE 8 Property Value API Gravity 21 N, ppm 1140 S, wt % 2.3 Polycyclic Index (PCI) 2333 TBP Range, ° F. (° C.)  5 708 (376) 10 742 (394) 30 810 (432) 50 861 (461) 70 913 (489) 90 981 (527) 95 1008 (542) Entire Product 1069 (576)

The hydrocracking runs were operated in a pilot plant unit under 2300 psig (18,858 kPa) total pressure, 1.0 to 2.0 LHSV, and 5000 SCF/B once through hydrogen gas. The runs were operated in a pilot plant unit under 2300 psig (18,858 kPa) total pressure, 1.0 to 2.0 LHSV, and 5000 SCF/B once through hydrogen gas. The test results are summarized below in Table 9.

TABLE 9 Base Base Base Case Case Case A D B E F C G CAT, ° F. (60% conv.) Base −9 Base −9 −18 Base −6 Yields Compared to Comparative Base Cases, by cut point C₄ ⁻, wt % Base −0.4 Base −0.9 0.2 Base −0.5 C₅-180° F., vol % Base −0.1 Base −0.4 0.1 Base −1.2 180-380° F., vol % Base −1.6 Base −1.5 0.1 Base −4.5 380-530° F., vol % Base 0.8 Base 0.2 −0.3 Base 1.0 530-700° F., vol % Base 1.5 Base 2.0 0.5 Base 2.8 Heavy Middle Base 2.3 Base 2.3 0.3 Base 3.7 distillates (380-700° F.), vol %

All of the example catalysts were 6 to 18° F. more active than the commercial comparative catalyst samples. The catalyst samples D, E, and G gave significantly increased yields of heavy middle distillates and reduced yields of products having a cut point below 380° F. It is believed that the hydrocracking catalyst samples comprising H-BEA-150, with the unique distribution of larger domain sizes (and thus fewer faults), reduced the unselective cracking that produces more gas.

Example 7: Comparison and Exemplary Catalyst Preparation and Hydrocracking Performance

Comparative catalyst sample H was prepared according to the following procedure: 1.4 wt % beta zeolite (CP811C-300 from Zeolyst, denoted as ZE0106), 5.8 wt % USY (CBV 760 from Zeolyst), 71.3 wt % ASA (from Sasol), and 21.5 wt % pseudo-boehmite alumina powder were mixed well. To this mix, nickel nitrate hexahydrate dissolved in diluted nitric acid were added, so that the total mix contained 0.64 wt % nitric acid, 12.5 wt % nickel nitrate hexahydrate and 43% deionized water. To this mix an ammonium metatungstate solution (54.5 w % ammonium metatungstentate in water) was added, with enough water to yield an extrudable mix, or paste. The paste was extruded and dried at 130° C. for one hour and calcined at 510° C. for one hour with purging excess dry air. After cooling down to room temperature the catalyst contained 5.2 wt % NiO and 25.2% WO₃ on a dry basis.

Catalyst Sample I was prepared by following the procedure of comparative catalyst sample H except that H-BEA-150 ZE0090 was used instead of ZE0106.

The hydrocracking performance of these two catalyst samples, H and I, were tested in a pilot plant unit under the same hydrocracking conditions. The catalyst sample I gave significantly decreased gas yields. Additionally, at the same 55 wt % conversion at 700° F., the hydrocracked effluent using the comparative sample H had a much lower waxy VI (at least 5 lower) than the effluent using the example catalyst I, 128 versus 137, respectively. Waxy VI was measured by ASTM D2270-10 (E 2011).

Example 1a: Preparation of Catalyst Sample DJ-4

Catalyst sample DJ-4 was prepared by combining 2.9 wt % H-BEA-150 zeolite, 1.1 wt % USY zeolite, 74.5 wt % amorphous silica alumina (ASA) powder, and 21.5 wt % pseudo-boehmite alumina; and mixing them well. The H-BEA-150 zeolite was a zeolite beta that was obtained from SUD CHEM IE. The USY zeolite was obtained from Zeolyst. The USY zeolite had an acid site distribution index (ASDI) of 0.086. Additional properties of the USY zeolite are summarized in Table 10.

TABLE 10 Brönsted acid sites determined by FTIR after H/D exchange (mmol/g) HF(OD) 0.076 HF′(OD) 0.005 LF(OD) 0.034 LF′(OD) 0.003 Total 0.118 ASDI 0.086

The ASA powder was Siral-40 obtained from Sasol. The pseudo-boehmite alumina was CATAPAL B from Sasol.

To this mixture described above, a diluted HNO₃ acid aqueous solution (2 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ (1.59 mm) asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 4.1 wt % NiO and 25.2 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for 1 hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished catalyst sample DJ-4 is shown in Table 11.

Example 2a: Preparation of Catalyst Sample DJ-5

Catalyst sample DJ-5 was prepared similar to the process described in Example 1. 5.7 wt % H-BEA-150 zeolite, 2.1 wt % USY zeolite, 70.7 wt % ASA powder, and 21.5 wt % pseudo-boehmite alumina powder were combined and mixed well. To this mixture, a diluted HNO₃ acid aqueous solution (2 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 4.1 wt % NiO and 25.2 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for 1 hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished catalyst sample DJ-5 is shown in Table 11.

Example 3a: Preparation of Catalyst Sample YY-8

Catalyst sample YY-8 was prepared by combining 1.6 wt % H-BEA-150 zeolite, 58.4 wt % amorphous silica alumina (ASA) powder, and 40 wt % pseudo-boehmite alumina; and mixing them well. To this mixture, a diluted HNO₃ acid aqueous solution (2 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel carbonate at concentrations to achieve the target metal loadings of 5 wt % NiO and 29 wt % WO₃, based on the bulk dry weight of the finished catalyst. The solution additionally contained 12.7 grams of citric acid as a chelating agent. The metal impregnated extruded catalyst was dried at 212° F. (100° C.) for 2 hours. The dried catalyst was then calcined at 500° F. (260° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished comparative catalyst sample YY-8 is shown in Table 11.

Example 4a: Preparation of Catalyst Sample YY-9

Catalyst sample YY-9 was prepared similar to the process described in Example 1. 7.1 wt % H-BEA-150 zeolite, 0.7 wt % USY zeolite, 70.7 wt % ASA powder, and 21.5 wt % pseudo-boehmite alumina powder were combined and mixed well. To this mixture, a diluted HNO₃ acid aqueous solution (2 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 4.1 wt % NiO and 25.2 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for 1 hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this finished catalyst sample YY-9 is shown in Table 11.

Example 5a: Preparation of Comparative Catalyst Sample

Comparative catalyst sample was prepared by combining 5.7 wt % USY zeolite, 71.3 wt % amorphous silica alumina (ASA) powder, and 23 wt % pseudo-boehmite alumina; and mixing them well.

To this mixture described above, a diluted HNO₃ acid aqueous solution (2 wt %) was added to form an extrudable paste. The extrudable paste was extruded into a 1/16″ asymmetric quadrolobe shape, and dried at 248° F. (120° C.) for 1 hour. The dried extrudates were calcined at 1100° F. (593° C.) for 1 hour with purging excess dry air, and cooled down to room temperature.

Ni and W were impregnated onto the dried extruded catalyst using a solution containing ammonium metatungstate and nickel nitrate at concentrations to achieve the target metal loadings of 3.8 wt % NiO and 25.3 wt % WO₃, based on the bulk dry weight of the finished catalyst. The metal impregnated extruded catalyst was dried at 270° F. (132° C.) for ½ hour. The dried catalyst was then calcined at 950° F. (510° C.) for 1 hour with purging excess dry air, and cooled down to room temperature. The composition of this comparative catalyst sample is shown in Table 11.

TABLE 11 Catalyst Compositions Comparative Catalyst Component Base Case DJ-4 DJ-5 YY-8 YY-9 Zeolite beta, wt % 0 2 4 1 5 Zeolite USY, wt % 4 0.8 1.5 0 0.5 NiO, wt % 3.8 4.1 4.1 5 4.1 WO₃, wt % 25.2 25.2 25.2 29 25.2 Al₂O₃ 67.0 67.9 65.2 Bal. 65.7 Citric Acid/Ni 0 0 0 0.6 0 Weight ratio zeolite — 0.40 0.375 0 0.10 USY/zeolite beta

Example 6a: Comparison of Catalyst Performance

The example catalysts described above were used to process a typical Middle Eastern VGO feedstock. The example catalysts were not presulfided.

The properties of the Middle Eastern VGO feedstock are described in Table 8 (see Example 6).

The hydrocracking runs were operated in a pilot plant unit under 2300 psig (18,858 kPa) total pressure, 1.0 to 2.0 LHSV, and 5000 SCF/B once through hydrogen gas. The test results are summarized below in Table 12.

TABLE 12 Comparative Base Case DJ-4 DJ-5 YY-8 YY-9 CAT, ° F. Base −5 −8 0 −12 (60% conv.) Yields Compared to Comparative Base Case, by cut point C₄ ⁻ gas, wt % Base −0.3 −0.2 −0.6 −0.6 C₅-180° F., vol % Base −0.6 0.1 −0.8 −0.8 180-380° F., vol % Base −6.7 −6.2 −7.5 −6.5 380-530° F., vol % Base 1.6 0.8 1.9 1.2 530-700° F., vol % Base 5.5 3.8 6.8 5.8 Heavy Middle distillates Base 7.1 4.6 8.7 7.0 (380-700° F.), vol %

The catalyst samples DJ-4, DJ-5, YY-8 and YY-9 gave significantly increased yields of middle distillates and reduced yields of products having a cut point below 380° F. compared to the commercial comparative catalyst sample. The catalyst examples containing similar total zeolite amounts of 4.0 to 5.5 wt % were 8 to 12° F. more active than the commercial comparative catalyst sample.

It is believed that the hydrocracking catalyst samples comprising H-BEA-150, with the unique distribution of larger domain sizes (and thus fewer faults), reduced the unselective cracking that produces more gas. The combination with a zeolite USY having minimum hyper-active sites (i.e., having an ASDI between 0.05 and 0.12) also provided enhanced activity.

Example 7a: Domain Size Analysis of Two Different Beta Zeolites

Domain size determinations were made on two samples of commercial zeolite beta. One sample was the same H-BEA-150 zeolite beta (ZE0090) used in the previous examples. The other sample was a comparison zeolite beta from Zeolyst International (CP811C-300, ZE0106) that had a higher SAR than H-BEA-150. The raw data and statistical analysis of the data for the domain size analysis is summarized in Table 13.

TABLE 13 Sample ZE0090 ZE0106 Mean 1089.9 663.6 Standard Error 119.2 67.8 Median 907.2 530.2 Standard Deviation 715.5 454.8 Sample Variance 511881.8 206846.9 Kurtosis 1.2 7.8 Skewness 1.1 2.6 Range 2972.4 2358.0 Minimum 207.7 205.8 Maximum 3180.1 2563.8 Sum 39236.8 29862.5 Count 36.0 45.0 Count of Small Domains, 200 to 600 nm² 8 20 Count of Large Domains, 1200 to 2000 nm² 11 1 Count of Extra Large Domains, 1500 to 3200 nm² 9 2

The data from these domain size analyses were also charted and are shown in FIGS. 2 and 3. FIG. 2 shows the differences in the frequency of the domain sizes between the two zeolite betas. FIG. 3 shows that the domain sizes for the H-BEA-150 were larger and more broadly distributed than those shown for the comparison zeolite beta. The standard deviation for the domain sizes for the H-BEA-150 was greater than 700 nm², while the standard deviation for the domain sizes for the comparison zeolite beta was less than 500 nm². Also, the H-BEA-150 zeolite beta had more large domains that had a domain size from 1200 to 2000 nm² than small domains that had a domain size from 200 to 600 nm²; which is notably different that the distribution of the domain sizes in the comparison zeolite beta. The H-BEA-150 had a similar distribution (9 vs. 8) of extra large domains with a domain size from 1500 to 3200 nm² to small domains with a domain size from 200 to 600 nm². In this context, similar distribution means that the ratio of the count of domains in the two different domain size ranges is from 0.8:1 to 1.2:1.

The transitional term “comprising”, which is synonymous with “including,” “containing,” or “characterized by,” is inclusive or open-ended and does not exclude additional, unrecited elements or method steps. The transitional phrase “consisting of” excludes any element, step, or ingredient not specified in the claim. The transitional phrase “consisting essentially of” limits the scope of a claim to the specified materials or steps “and those that do not materially affect the basic and novel characteristic(s)” of the claimed invention.

For the purposes of this specification and appended claims, unless otherwise indicated, all numbers expressing quantities, percentages or proportions, and other numerical values used in the specification and claims, are to be understood as being modified in all instances by the term “about.” Furthermore, all ranges disclosed herein are inclusive of the endpoints and are independently combinable. Whenever a numerical range with a lower limit and an upper limit are disclosed, any number falling within the range is also specifically disclosed. Unless otherwise specified, all percentages are in weight percent.

Any term, abbreviation or shorthand not defined is understood to have the ordinary meaning used by a person skilled in the art at the time the application is filed. The singular forms “a,” “an,” and “the,” include plural references unless expressly and unequivocally limited to one instance.

All of the publications, patents and patent applications cited in this application are herein incorporated by reference in their entirety to the same extent as if the disclosure of each individual publication, patent application or patent was specifically and individually indicated to be incorporated by reference in its entirety.

This written description uses examples to disclose the invention, including the best mode, and also to enable any person skilled in the art to make and use the invention. Many modifications of the exemplary embodiments of the invention disclosed above will readily occur to those skilled in the art. Accordingly, the invention is to be construed as including all structure and methods that fall within the scope of the appended claims. Unless otherwise specified, the recitation of a genus of elements, materials or other components, from which an individual component or mixture of components can be selected, is intended to include all possible sub-generic combinations of the listed components and mixtures thereof.

The invention illustratively disclosed herein suitably may be practiced in the absence of any element which is not specifically disclosed herein. 

What is claimed:
 1. A hydrocracking catalyst comprising: a zeolite beta having an average domain size from 800 to 1500 nm²; a zeolite USY; a catalyst support; and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table, wherein, the zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY; and the zeolite beta has an OD acidity of 20 to 400 μmol/g and the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 and the zeolite USY content is from 0 to 5 wt. % when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY.
 2. The hydrocracking catalyst of claim 1, wherein the zeolite beta has a SiO₂/Al₂O₃ ratio (SAR) from 50 to
 200. 3. The hydrocracking catalyst of claim 1, wherein the zeolite beta OD acidity is from 30 to 40 μmol/g when the weight percentage content of the zeolite beta in the catalyst is less than the weight percentage of the zeolite USY.
 3. The hydrocracking catalyst of claim 1, wherein the zeolite beta OD acidity is from 30 to 100 μmol/g when the weight percentage content of the zeolite beta in the catalyst is greater than the weight percentage of the zeolite USY.
 4. The hydrocracking catalyst of claim 1, wherein the average domain size is from 900 to 1250 nm².
 5. The hydrocracking catalyst of claim 1, wherein the zeolite beta has more large domains that have a domain size from 1200 to 2000 nm² than small domains that the domain size from 200 to 600 nm².
 6. The hydrocracking catalyst of claim 1, wherein the zeolite beta has a standard deviation of domain sizes greater than 700 nm².
 7. The hydrocracking catalyst of claim 1, wherein a weight ratio of the zeolite beta to the zeolite USY is from 0.10 to 0.95.
 8. The hydrocracking catalyst of claim 1, wherein the wt. % of the zeolite beta is from 1 to 5 wt. % higher than the wt. % of the zeolite USY.
 9. The hydrocracking catalyst of claim 1, wherein the zeolite USY has an ASDI between 0.05 and 0.12.
 10. The hydrocracking catalyst of claim 1, wherein a weight ratio of the zeolite USY to the zeolite beta is 0 to 0.48.
 11. The hydrocracking catalyst of claim 1, wherein the second support is a pseudo-boehmite alumina.
 12. The hydrocracking catalyst of claim 1, wherein the zeolite USY has a total Brönsted acid sites content determined by FTIR after H/D exchange of 0.080 to 0.200 mmol/g.
 13. The hydrocracking catalyst of claim 1, comprising at least one Group 6 metal and at least one metal selected from Groups 8 through 10 of the Periodic Table.
 14. A process for hydrocracking a hydrocarbonaceous feedstock, comprising contacting the hydrocarbonaceous feedstock with a hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent that comprises middle distillates; wherein the hydrocracking catalyst comprises: a zeolite beta having an average domain size from 800 to 1500 nm²; a zeolite USY; a catalyst support; and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table, wherein, the zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY; and the zeolite beta has an OD acidity of 20 to 400 μmol/g and the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 and the zeolite USY content is from 0 to 5 wt. % when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY.
 15. The process of claim 14, wherein the hydrocarbonaceous feedstock has a TBP within 700 to 1200° F. (371 to 649° C.).
 16. The process of claim 14, wherein the zeolite beta has a SiO₂/Al₂O₃ ratio (SAR) from 50 to
 200. 17. The process of claim 14, wherein the zeolite beta OD acidity is from 30 to 40 μmol/g when the weight percentage content of the zeolite beta in the catalyst is less than the weight percentage of the zeolite USY.
 18. The process of claim 14, wherein the zeolite beta OD acidity is from 30 to 100 μmol/g when the weight percentage content of the zeolite beta in the catalyst is greater than the weight percentage of the zeolite USY.
 19. The process of claim 14, wherein the average domain size is from 900 to 1250 nm².
 20. The process of claim 14, wherein the zeolite beta has more large domains that have a domain size from 1200 to 2000 nm² than small domains that have the domain size from 200 to 600 nm².
 21. The process of claim 14, wherein the zeolite beta has a standard deviation of domain sizes greater than 700 nm².
 22. The process of claim 14, wherein a weight ratio of the zeolite beta to the zeolite USY is from 0.10 to 0.95.
 23. The process of claim 14, wherein the wt. % of the zeolite beta is from 1 to 5 wt. % higher than the wt. % of the zeolite USY.
 24. The process of claim 14, wherein the zeolite USY has an ASDI between 0.05 and 0.12.
 25. The process of claim 14, wherein a weight ratio of the zeolite USY to the zeolite beta is 0 to 0.48.
 26. The process of claim 14, wherein the second support is a pseudo-boehmite alumina.
 27. The process of claim 14, wherein the zeolite USY has a total Brönsted acid sites content determined by FTIR after H/D exchange of 0.080 to 0.200 mmol/g.
 28. The process of claim 14, comprising at least one Group 6 metal and at least one metal selected from Groups 8 through 10 of the Periodic Table.
 29. The process of claim 14, wherein the hydrocracked effluent comprises from greater than 50 vol % to 95 vol % of a heavy middle distillate having a TBP of 380-700° F. (193-371° C.) when the weight percentage content of the zeolite beta in the catalyst is less than the weight percentage of the zeolite USY; or from greater than 30 vol % to 50 vol % of a heavy middle distillate having a TBP of 380-700° F. (193-371° C.) when the weight percentage content of the zeolite beta in the catalyst is greater than the weight percentage of the zeolite USY.
 30. A method for making a hydrocracking catalyst, comprising: mixing together a zeolite beta having an average domain size from 800 to 1500 nm²; a zeolite USY; a catalyst support; and enough liquid to form an extrudable paste; wherein, the zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY; and the zeolite beta has an OD acidity of 20 to 400 μmol/g and the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 and the zeolite USY content is from 0 to 5 wt. % when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY; extruding the extrudable paste to form an extrudate base; impregnating the extrudate base with a metal impregnation solution containing at least one metal selected from the group consisting of elements from Group 6 and Group 8 through 10 of the Periodic Table to make a metal-loaded extrudate; and post-treating the metal-loaded extrudate by subjecting the metal-loaded extrudate to drying and calcination; wherein the hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 380-700° F. (193-371° C.). 